WO2012095976A1

WO2012095976A1 - Device for producing sugar solution, fermentation system, method for producing sugar solution and fermentation method

Info

Publication number: WO2012095976A1
Application number: PCT/JP2011/050448
Authority: WO
Inventors: 稔源田; 寺倉　誠一; 英夫鈴木; 岳近藤; 理郎西山
Original assignee: 三菱重工メカトロシステムズ株式会社
Priority date: 2011-01-13
Filing date: 2011-01-13
Publication date: 2012-07-19
Also published as: AU2011355013B2; AU2011355013A1; US20130196424A1; JP4875785B1; CA2791665A1; US9434971B2; CA2791665C; US9102965B2; BR112012028430B1; BR112012028430A2; US20120315677A1; JPWO2012095976A1

Abstract

A device (11A) for producing a sugar solution (22) derived from a carbohydrate-based starting material (21), said device comprising: a sugar solution preparation part (15A) for preparing the sugar solution (22) derived from the carbohydrate-based starting material (21); a cellulose-based biomass saccharification part (16) for saccharifying a hydrothermally treated biomass, which is obtained by hydrothermally decomposing a cellulose-based starting biomass material (35) containing a lignin component and a hemicellulose component, to give a dilute sugar solution (37); and a dilute sugar solution-supply pipe (L11) for supplying the dilute sugar solution (37), which is produced in the cellulose-based biomass saccharification part (16), to the sugar solution preparation part (15A). According to this constitution, the productivity of the sugar solution (22) can be improved and the production cost thereof can be reduced.

Description

Sugar solution manufacturing apparatus, fermentation system, sugar solution manufacturing method and fermentation method

The present invention relates to a sugar liquid production apparatus, a fermentation system, a sugar liquid production method, and a fermentation method for producing a sugar liquid derived from a carbohydrate-based raw material, and more specifically, the production efficiency of the sugar liquid when producing a sugar liquid from a carbohydrate-based raw material Is to improve.

Biomass, which is an organic resource derived from living organisms, is a resource that living organisms produce from water and carbon dioxide using solar energy, and is a resource that can be continuously regenerated. In recent years, as part of measures against global warming, attempts have been widely made to produce ethanol from biomass containing cellulosic raw materials such as woody biomass and herbaceous biomass and use them as various fuels and chemical raw materials. Biomass ethanol produced from biomass is a natural energy that can be recycled, and biomass is attracting attention as an effective resource that can be used from the viewpoint of not increasing carbon dioxide released into the atmosphere by burning biomass ethanol. And is expected to be used as a future energy source.

Biomass refers to the accumulation of organisms incorporated in the material circulation system of the Earth's biosphere or organic matter derived from organisms (see JIS K 3600 1258). Biomass includes, for example, forestry (sawmill waste, thinned wood, paper waste, etc.), agriculture (rice straw, straw, sugarcane straw, rice straw, coconut shell, vegetation, etc.), livestock (livestock waste, etc.), It is classified into fisheries (fishery processing residue, etc.), waste (garbage, garden trees, construction waste, sewage sludge, etc.).

Conventionally, as a method for producing ethanol, a method of producing ethanol by saccharifying biomass containing a carbohydrate-based raw material or a cellulose-based raw material to produce a sugar solution, and fermenting the obtained sugar solution is used. . As a method for producing ethanol using biomass, for example, sulfuric acid is added to the collected biomass for hydrolysis, the biomass is decomposed into sugar, solid-liquid separation is performed, the liquid phase is neutralized, and neutralization is performed. A method for producing ethanol (for example, refer to Patent Documents 1 and 2) in which the liquid phase is subjected to ethanol fermentation using a microorganism such as yeast and converted to ethanol, or the collected biomass and pressurized hot water are brought into contact in a compacted state. Ethanol that hydrolyzes and obtains a hydrothermally processed biomass, adds an enzyme to the obtained biomass hydrothermally processed material to obtain a saccharified solution, and ferments the obtained saccharide solution to produce ethanol Have been proposed (for example, see Patent Documents 3 and 4).

JP-T 9-507386 Japanese National Patent Publication No. 11-506934 JP 2010-29862 A JP 2010-82620 A

Here, high sugar recovery is achieved when an enzyme is added to a biomass hydrothermal treatment product obtained from biomass using a method of hydrothermally decomposing biomass such as Patent Documents 3 and 4 using pressurized hot water. It is required to secure the rate and increase the sugar concentration of the produced sugar solution. Therefore, in order to produce a sugar solution having a high sugar concentration, it is necessary to increase the concentration of the biomass hydrothermal treatment material as a raw material when an enzyme is added to the biomass hydrothermal treatment material for saccharification.

However, when the concentration of the biomass hydrothermally treated product is increased, there is a problem that the sugar recovery rate is decreased due to a poor mixing state between the biomass hydrothermally treated product and the enzyme.

In addition, when the concentration of the biomass hydrothermal treatment is high, the power required to stir the biomass hydrothermal treatment in the enzyme saccharification tank containing the biomass hydrothermal treatment is increased. There is a problem that required power consumption increases.

Furthermore, in order to increase the sugar yield in a state where the concentration of the biomass hydrothermal treatment is high, a method of adding an excess of enzyme can be considered, but since the enzyme used to saccharify the biomass hydrothermal treatment has a high unit price, When the amount of enzyme added to the biomass hydrothermal treatment increases, there is a problem that the cost required for producing ethanol increases.

Therefore, after saccharifying the biomass hydrothermally treated product, for example, it is generally subjected to a concentration operation such as evaporative concentration in order to obtain a predetermined concentration suitable for fermentation, for example, for alcohol fermentation.

On the other hand, when various organic raw materials are produced from sugar liquid derived from carbohydrate-based raw materials (such as those by saccharification or extraction / exploitation), for example, in an alcohol fermentation system equipped with a sugar liquid production apparatus, the sugar liquid used for fermentation If the concentration is high, the atmosphere becomes high in alcohol concentration as the fermentation progresses, and the microorganism that performs the fermentation is killed, so that it cannot be used as it is for alcohol fermentation. Therefore, it was necessary to prepare the sugar solution by diluting the above-mentioned sugar solution (sugar concentration of about 20 to 60%) with water.

Therefore, there is a need for an efficient system that can solve both of the problems in producing sugar by the biomass treatment and various organic raw materials from the sugar liquid derived from the carbohydrate raw material.

In view of the above problems, an object of the present invention is to provide a sugar solution production apparatus, a fermentation system, a sugar solution production method, and a fermentation method capable of improving the production efficiency of a sugar solution and reducing the cost. .

A first invention of the present invention for solving the above-described problem is a sugar liquid production apparatus for producing a sugar liquid derived from a carbohydrate-based raw material, wherein the sugar liquid adjustment is performed to adjust the sugar liquid derived from the carbohydrate-based raw material A cellulose-based biomass saccharification unit that saccharifies a biomass hydrothermal treatment product obtained by hydrothermally decomposing a cellulosic biomass raw material containing a lignin component and a hemicellulose component, and the cellulose-based biomass saccharification unit And a diluted sugar solution supply pipe for mixing the diluted sugar solution manufactured in (1) with the sugar solution adjusting unit.

A second invention is the sugar solution production apparatus according to the first invention, wherein the sugar solution is obtained by saccharification of the carbohydrate-based material, or extracted or extracted from the carbohydrate-based material. .

3rd invention is 1st or 2nd invention. WHEREIN: The said cellulose biomass saccharification part hydrothermally heats the said cellulose biomass raw material, and produces | generates biomass hydrothermal treatment, The said biomass hydrothermally processed material And a second enzyme saccharification tank for saccharifying the biomass hydrothermal treatment product to produce the diluted sugar solution.

In a fourth aspect based on the third aspect, the hydrothermal decomposition apparatus hydrothermally decomposes the cellulosic biomass raw material in contact with pressurized hot water, and a lignin component and a hemicellulose component in the pressurized hot water. And separating the lignin component and hemicellulose component from the cellulosic biomass raw material, as the biomass hydrothermal treatment, a hydrothermal extraction fraction containing the lignin component and hemicellulose component, and a solid residue fraction containing the cellulose component This is a sugar liquid production apparatus for producing a minute.

According to a fifth invention, in the fourth invention, the second enzyme saccharification tank adds an enzyme to the solid residue fraction discharged from the hydrothermal decomposition apparatus, and the cellulose component in the solid residue fraction Is added to the dilute sugar solution containing 6 carbon sugars and the hydrothermal extraction fraction discharged from the hydrothermal decomposition apparatus, and the hemicellulose component in the hydrothermal extraction fraction is enzymatically decomposed. This is a sugar solution production apparatus for producing either or both of a diluted sugar solution containing pentose.

A sixth invention is the sugar liquid production apparatus according to any one of the first to fifth inventions, wherein a sugar concentration of the diluted sugar liquid is 0.1% by mass or more and 15% by mass or less.

A seventh invention is a fermentation system comprising: the sugar solution producing apparatus according to any one of the first to sixth inventions; and an alcohol fermenter that ferments the sugar solution to produce an organic raw material. is there.

The eighth invention is a sugar liquid production method for producing a sugar liquid derived from a carbohydrate-based raw material, which is obtained by hydrothermally decomposing a cellulosic biomass raw material containing a lignin component and a hemicellulose component to produce a biomass hydrothermal treatment product. In addition, an enzyme is added to the biomass hydrothermal treatment product to saccharify the biomass hydrothermal treatment product to produce a diluted sugar solution, and the diluted sugar solution is used when adjusting the sugar solution derived from the carbohydrate-based raw material. A method for producing a sugar solution, comprising producing the sugar solution.

A ninth invention is the method for producing a sugar liquid according to the eighth invention, wherein as the sugar liquid, one obtained by saccharification of the carbohydrate-based raw material or one extracted or extracted from the carbohydrate-based raw material is used. .

The tenth invention is the eighth or ninth invention, wherein the cellulosic biomass raw material is hydrothermally decomposed in contact with pressurized hot water, the lignin component and the hemicellulose component are transferred to the pressurized hot water, Separating the lignin component and the hemicellulose component from the cellulosic biomass raw material, producing a hydrothermal extraction fraction containing the lignin component and the hemicellulose component, and a solid residue fraction containing the biomass solid content, as the biomass hydrothermal treatment, It is a sugar liquid manufacturing method using either one or both of the hydrothermal extraction fraction and the solid residue fraction.

An eleventh aspect of the invention is the diluted sugar liquid according to the tenth aspect of the invention, in which an enzyme is added to the solid residue fraction as the diluted sugar liquid, and the cellulose in the solid residue fraction is enzymatically decomposed to contain hexose. In the method for producing a sugar solution, an enzyme is added to the hydrothermal extract fraction, and the hemicellulose component in the hydrothermal extract fraction is enzymatically decomposed to use one or both of a dilute sugar solution containing pentose. is there.

A twelfth aspect of the invention is a sugar solution manufacturing method according to any one of the eighth to eleventh aspects, wherein the sugar concentration of the diluted sugar solution is 0.1% by mass or more and 15% by mass or less.

A thirteenth invention is a fermentation method characterized by fermenting a sugar liquid obtained using any one of the sugar liquid production methods of any one of the eighth to twelfth inventions to produce an organic raw material. is there.

Furthermore, in order to solve the above-mentioned problem, the following configuration can also be adopted.
(1) That is, when the sugar solution is obtained by saccharifying the carbohydrate-based raw material, the sugar liquid adjusting unit is configured to store the carbohydrate-based raw material in a storage tank, and to enzymatically saccharify the carbohydrate-based raw material. It is good also as a sugar solution manufacturing apparatus characterized by having a 1st enzyme saccharification tank.

(2) When the sugar liquid is extracted or extracted from the carbohydrate-based raw material, the sugar liquid adjusting unit has a storage tank for storing the carbohydrate-based raw material and a sugar concentration adjusting tank. It is good also as a sugar liquid manufacturing apparatus.

(3) When the sugar solution is obtained by saccharifying the carbohydrate-based raw material, the sugar solution is stored in a storage tank for storing the carbohydrate-based raw material, and a first enzyme for enzymatically saccharifying the carbohydrate-based raw material It is good also as a sugar liquid manufacturing method characterized by adding to any one or both with a saccharification tank.

(4) In the case where the sugar liquid is extracted or extracted from the carbohydrate-based raw material, the sugar liquid is placed in one or both of a storage tank for storing the carbohydrate-based raw material and a sugar concentration adjusting tank. It is good also as a manufacturing method of the sugar liquid characterized by adding.

According to the present invention, it is possible to improve the production efficiency of the sugar liquid and reduce the cost.

FIG. 1 is a schematic diagram of an alcohol production system including a sugar liquid production apparatus according to Embodiment 1 of the present invention. FIG. 2 is a diagram showing the configuration of the hydrothermal decomposition apparatus. FIG. 3 is a diagram showing another configuration of the hydrothermal decomposition apparatus. FIG. 4 is a diagram illustrating an example in which corn is used as a raw material. FIG. 5 is a schematic view of an alcohol production system including a sugar liquid production apparatus according to Example 2 of the present invention. FIG. 6 is a diagram illustrating an example in which sugarcane is applied as a raw material.

Embodiments of the present invention will be described in detail with reference to the drawings. The present invention is not limited by the contents described in the following examples. The constituent elements described below include those that can be easily assumed by those skilled in the art, those that are substantially the same, and those that are so-called equivalent ranges. Furthermore, the constituent elements described below can be appropriately combined.

The sugar liquid production apparatus according to Example 1 of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram of an alcohol production system including a sugar liquid production apparatus according to Embodiment 1 of the present invention. As shown in FIG. 1, the alcohol production system 10 A includes a sugar liquid production apparatus 11 A according to the present embodiment, an alcohol fermentation tank 12, a distillation tower 13, and an alcohol tank 14.

The sugar solution manufacturing apparatus 11A according to the present embodiment includes a sugar solution adjusting unit 15A and a cellulose biomass saccharification unit 16.

(Sugar solution adjuster)
The sugar liquid adjusting unit 15 A manufactures the sugar liquid 22 from the carbohydrate-based raw material 21. The sugar liquid adjusting unit 15A includes a pulverizer 23, a fine pulverizer 24, a storage tank 25, a steamer 26, and a first enzyme saccharification tank 27. The carbohydrate-based raw material 21 is pulverized by a pulverizer 23 and further pulverized by a fine pulverizer 24. The finely pulverized carbohydrate-based raw material 21 is stored in the storage tank 25. The carbohydrate-based raw material 21 stored in the storage tank 25 is steamed by the steamer 26 and then saccharified by adjusting the sugar concentration in the first enzyme saccharification tank 27. In the present embodiment, a diluted sugar solution 37 (described later) is added to either one or both of the storage tank 25 and the first enzyme saccharification tank 27, and used as a diluted solution when the sugar solution 22 is produced from the carbohydrate-based raw material 21. Use. As will be described later, the carbohydrate-based raw material 21 is diluted with the diluted sugar solution 37 by adding the diluted sugar solution 37 to the storage tank 25. Thereby, the carbohydrate-based raw material 21 in the storage tank 25 can be easily saccharified and transported easily in the first enzyme saccharification tank 27.

(Cellulose biomass saccharification department)
The cellulosic biomass saccharification unit 16 includes a pulverizer 31, a hydrothermal decomposition apparatus 32A, a second enzyme saccharification tank (C6) 33, and a second enzyme saccharification tank (C5) 34. The cellulosic biomass saccharification part 16 produces the diluted sugar liquid 37 by saccharifying the biomass hydrothermal treatment product obtained by hydrothermally decomposing the cellulosic biomass raw material 35.

Biomass is not particularly limited, and refers to the accumulation of organisms incorporated into the material circulation system of the Earth's biosphere or organic substances derived from organisms (see JIS K 3600 1258). As the biomass, it is particularly preferable to use woody lignocellulosic resources such as hardwood, herbaceous, agricultural waste, food waste and the like. In the present embodiment, examples of the cellulosic biomass raw material 35 include rice straw, wheat straw, corn stover (corn stalk), corn cob (corn core), EFB (empty palm fruit bunches), and the like. However, the present embodiment is not limited to these.

The cellulose-based biomass material 35 is pulverized to, for example, 5 mm or less by the pulverizer 31 to become a biomass material pulverized product 38. The biomass raw material pulverized product 38 is hydrothermally treated by the hydrothermal decomposition apparatus 32A. The hydrothermal decomposition apparatus 32A hydrothermally decomposes the biomass raw material pulverized product 38 in contact with the pressurized hot water, transfers the lignin component and the hemicellulose component into the pressurized hot water, and the lignin component and hemicellulose from the biomass solid. The components are separated. The hydrothermally processed biomass is hydrothermally processed by hydrothermally treating the biomass raw material 38 with a hydrothermal decomposition apparatus 32A, and transferring a solid residue fraction 39, which is a biomass solid, and a lignin component and a hemicellulose component into pressurized hot water. Extracted fraction 40 is obtained.

The configuration of the hydrothermal decomposition apparatus 32A is shown in FIG. As shown in FIG. 2, the hydrothermal decomposition apparatus 32 A includes a biomass supply apparatus 41, a reaction apparatus 42, and a biomass extraction apparatus 43. The biomass supply device 41 supplies a cellulosic biomass material (hereinafter referred to as “biomass material”) 35 from normal pressure to pressure.

The reactor 42 transports the supplied biomass raw material 35 from either one (lower side in this embodiment) to the other (upward) by screw means 44 inside the main body of the apparatus, and supplies the biomass raw material 35. Pressurized hot water 45 is supplied into the inside of the apparatus main body from the other (upper) side different from the location, and hydrothermal decomposition is performed while the biomass raw material 35 and the pressurized hot water 45 are brought into contact with each other. Thereby, the lignin component and the hemicellulose component are transferred into the pressurized hot water 45, separated from the biomass raw material 35, and discharged from the reaction device 42 as the hydrothermal extraction fraction 40.

The biomass extraction device 43 extracts a solid residue fraction 39 that is a biomass solid content from the other of the reaction devices 42. In the figure, reference numeral 47 denotes a dehydrating liquid, 48 denotes pressurized nitrogen (N ₂ ), and 49 denotes a temperature jacket.

In the present embodiment, the biomass raw material 35 is supplied from the lower end side, but the present embodiment is not limited to this, and conversely, it may be supplied from the upper end side. At that time, the pressurized hot water 45 is supplied from the lower end side.

Examples of the biomass supply device 41 that supplies from normal pressure to increased pressure include means such as a screw feeder, a piston pump, and a slurry pump.

The reaction apparatus 42 is a vertical apparatus in the present embodiment, but the present embodiment is not limited to this, and may be an inclined apparatus or a horizontal apparatus. Here, the vertical type and the inclined type are preferable because the gas generated in the hydrothermal decomposition reaction, the gas brought into the raw material, and the like can quickly escape from above. In addition, since the decomposition product is extracted with the pressurized hot water 45, the concentration of the extract increases from the upper side to the lower side in terms of extraction efficiency, which is preferable.

In this embodiment, before the biomass is supplied, pretreatment is performed using a pulverizer 31 as a pretreatment device. However, the present embodiment is not limited to this, and particles of the biomass material 35 When the diameter is sufficiently small, the pulverizer 31 may not be provided. Moreover, you may make it wash | clean with a washing | cleaning apparatus. In addition, when the biomass raw material 35 is, for example, rice husk or the like, it can be supplied to the reactor 42 as it is without being pulverized.

The reaction temperature in the reactor 42 is preferably 180 ° C. or higher and 240 ° C. or lower. More preferably, it is 200 degreeC or more and 230 degrees C or less. This is because at a low temperature of less than 180 ° C., the hydrothermal decomposition rate is low, a long decomposition time is required, leading to an increase in the size of the apparatus, which is not preferable. On the other hand, when the temperature exceeds 240 ° C., the decomposition rate becomes excessive, the cellulose component increases the transition from the solid to the liquid side, and the excessive decomposition of the hemicellulose saccharide is promoted, which is not preferable. The hemicellulose component dissolves from about 140 ° C., the cellulose from about 230 ° C., and the lignin component from about 140 ° C., but the cellulose remains on the solid side, and the hemicellulose component and the lignin component have a sufficient decomposition rate. It is good to set it as the range of 180 to 240 degreeC which it has.

The reaction pressure is preferably set to a higher pressure of 0.1 MPa to 0.5 MPa than the saturated vapor pressure of water at each temperature at which the inside of the main body is in the state of pressurized hot water.

The reaction time is preferably 20 minutes or less, more preferably 3 minutes or more and 10 minutes or less. This is because if the reaction is carried out too long, the proportion of the overdecomposed product increases, which is not preferable.

In the present embodiment, the flow of the pressurized hot water 45 and the biomass raw material 35 in the main body of the reactor 42 is a so-called counter flow in which the biomass raw material 35 and the pressurized hot water 45 are brought into contact with each other in a so-called counter flow. It is preferable to do so.

In the reactor 42, the solid content of the biomass raw material 35 is supplied from the bottom side, and the pressurized hot water 45 is supplied from the top side. ) 45 is moved while oozing between solid particles in the solid biomass material 35 and the counter flow.

In this embodiment, since a gas portion exists inside the reaction apparatus 42, pressurized nitrogen (N ₂ ) 48 is supplied to the inside, but the present invention is limited to this. The pressurized N ₂ 48 may not be supplied to the inside of the reaction device 42.

The temperature of the biomass raw material 35 in the reaction device 42 can be raised by contacting the pressurized hot water 45 in the reaction device 42 and directly exchanging heat. In addition, you may make it heat using water vapor | steam etc. from the outside as needed.

In this embodiment, the biomass raw material 35 and the pressurized hot water 45 are brought into contact with each other so that the components that are easily solubilized in the pressurized hot water 45 are discharged sequentially, and hot water is supplied from the input portion of the biomass raw material 35. Since a temperature gradient is generated up to the charging portion, the excessive decomposition of the hemicellulose component is suppressed, and as a result, the pentose component can be efficiently recovered. Furthermore, heat recovery can be achieved by making the opposite contact, which is preferable from the viewpoint of system efficiency.

The hydrothermal decomposition apparatus 32A is not limited to the configuration shown in FIG. FIG. 3 is a conceptual diagram showing another configuration of the hydrothermal decomposition apparatus. As shown in FIG. 3, the biomass hydrothermal decomposition apparatus 32 B according to the present embodiment includes a biomass supply apparatus 51, a reaction apparatus 52, and a biomass extraction apparatus 43. V31 to V35 indicate differential pressure regulating valves (ON-OFF valves).

The biomass supply device 51 is a device that supplies a biomass raw material 35 (for example, straw or the like in the present embodiment) from under normal pressure to under pressure. Examples of the biomass supply device 51 include pump means such as a piston pump or a slurry pump.

The reactor 52 gradually supplies the supplied biomass raw material 35 from one of the upper and lower end sides (the lower end side in this embodiment) to the inside of the vertical apparatus main body (hereinafter referred to as “apparatus main body”) in a consolidated state. While being moved, pressurized hot water 45 is supplied into the apparatus main body from the end side different from the supply of the biomass raw material 35 (the upper end side in the present embodiment), and the biomass raw material 35 and the pressurized hot water 45 are opposed to each other. It is a reaction apparatus in which the lignin component and the hemicellulose component are transferred into the pressurized hot water 45 and separated from the biomass raw material 35 while being hydrothermally decomposed.

The biomass extraction apparatus 43 extracts the solid residue fraction 39, which is a biomass solid content, from the supply section side of the pressurized hot water 45 of the apparatus main body as described above.

A fixed stirring means 53 for stirring the biomass raw material 35 in a so-called plug flow compaction state is provided inside the apparatus main body. When the fixed agitation means 53 rotates, the biomass raw material 35 is agitated by the agitation action generated by the rotation of the fixed agitation means 53 when the biomass raw material 35 fed into the interior is moved in the axial direction. By providing the fixed stirring means 53 inside the apparatus main body, the mixing of the solid surface and the pressurized hot water 45 in the solid proceeds in the apparatus main body, and the reaction is promoted.

From the viewpoint of efficiently mixing the biomass material 35 and the pressurized hot water 45 and promoting the reaction, the flow of the pressurized hot water 45 and the biomass material 35 in the apparatus main body of the hydrothermal decomposition apparatus 32B is as follows. It is preferable to stir and flow by a so-called counter flow in which 35 and the pressurized hot water 45 are brought into contact with each other.

Since the hydrothermal decomposition apparatus 32B is a plug flow type hydrothermal decomposition, the structure is simple, and the biomass raw material 35 that is a solid moves in parallel with the tube center axis while being stirred perpendicularly to the tube center axis. It will be. On the other hand, pressurized hot water 45 (hot water, a solution in which a decomposition product is dissolved) moves while oozing between solid particles in a counter flow with respect to the solid.

In the plug flow, a uniform flow of the pressurized hot water 45 can be realized. When the solid biomass material 35 is decomposed by the pressurized hot water 45, the decomposition product is dissolved on the hot water side. The vicinity of the decomposition part becomes highly viscous, hot water moves preferentially to the vicinity of the undecomposed part, and the undecomposed part continues to decompose. Thereby, a uniform flow of hot water is formed, and uniform decomposition is realized.

The hydrothermal decomposition apparatus 32B has a fixed stirring means 53 in the apparatus main body. Due to the resistance of the tube wall on the inner surface of the apparatus main body in the hydrothermal decomposition apparatus 32B, the solid density on the outlet side of the biomass raw material 35 is reduced in the apparatus main body compared to the inlet side of the biomass raw material 35. The solid residue fraction 39 is reduced. For this reason, the ratio for which the pressurized hot water 45 occupies increases, and the liquid residence time increases, whereby the decomposition component in the liquid is excessively decomposed. For this reason, the hydrothermal decomposition apparatus 32B is provided with at least the fixed stirring means 53 in the apparatus main body, thereby suppressing the proportion of the pressurized hot water 45 and reducing the liquid residence time, thereby decomposing components in the liquid. Can be prevented from overdegrading.

As shown in FIG. 1, in the sugar liquid production apparatus 11A according to the present embodiment, the solid residue fraction 39 and the hydrothermal extraction fraction 40 are discharged from the hydrothermal decomposition apparatus 32A as a biomass hydrothermal treatment product. The solid residue fraction 39 of the biomass hydrothermal treatment product is fed to the second enzyme saccharification tank (C6) 33, and the hydrothermal extraction fraction 40 is fed to the second enzyme saccharification tank (C5) 34.

The second enzymatic saccharification tank (C6) 33 is a first enzyme containing 6 carbon sugars by enzymatic treatment of cellulose in the solid residue fraction 39 discharged from the hydrothermal decomposition apparatus 32A with the first enzyme (cellulase) 61. The sugar solution 62 is obtained.

The second enzyme saccharification tank (C5) 34 includes pentose by subjecting the hemicellulose component transferred into the hydrothermal extraction fraction 40 discharged from the hydrothermal decomposition apparatus 32A to enzymatic treatment with the second enzyme 63. The second sugar solution 64 is obtained.

Either or both of the first sugar solution 62 obtained in the second enzyme saccharification tank (C6) 33 and the second sugar solution 64 obtained in the second enzyme saccharification tank (C5) 34 are used. Used as a diluted sugar solution 37. As described above, the diluted sugar solution 37 is supplied to one or both of the storage tank 25 and the first enzyme saccharification tank 27 via the diluted sugar solution supply pipe L11.

The diluted sugar liquid supply pipe L11 includes a diluted sugar liquid supply pipe L11-1 connected to the second enzyme saccharification tank (C6) 33 and a diluted sugar liquid supply pipe L11 connected to the second enzyme saccharification tank (C5) 34. -2, a diluted sugar solution supply pipe L11-3 for supplying the diluted sugar solution 37 to the sugar solution adjusting unit 15A from the connecting portion of the diluted sugar solution supply pipe L11-1 and the diluted sugar solution supply pipe L11-2, A diluted sugar solution supply pipe L11-4 connecting the sugar solution supply pipe L11-3 and the storage tank 25, and a diluted sugar solution supply pipe connecting the diluted sugar solution supply pipe L11-3 and the first enzyme saccharification tank 27. L11-5.

The diluted sugar solution supply pipe L11-1 is provided with a control valve V11, the diluted sugar solution supply pipe L11-2 is provided with a control valve V12, and the diluted sugar solution supply pipe L11-4 is provided with a control valve V21. And a control valve V22 is provided in the diluted sugar liquid supply pipe L11-5. The amount of the first sugar solution 62 extracted from the second enzyme saccharification tank (C6) 33 is adjusted by the control valve V11, and the second sugar solution extracted from the second enzyme saccharification tank (C5) 34. The amount of 64 is adjusted by the control valve V12. Further, the diluted sugar solution 37 supplied to the storage tank 25 is adjusted by the control valve V21, and the diluted sugar solution 37 supplied to the first enzyme saccharification tank 27 is adjusted by the control valve V22.

Therefore, the diluted sugar liquid 37 produced | generated in the cellulose biomass saccharification part 16 can be supplied to either one or both of the storage tank 25 and the 1st enzyme saccharification tank 27 via the diluted sugar liquid supply pipe | tube L11. . That is, in the adjustment stage before the sugar-based raw material 21 is saccharified to generate the sugar liquid 22 in the sugar liquid adjusting unit 15A, for example, in this embodiment, the carbohydrate-based raw material 21 is pulverized by the pulverizer 23 and the fine pulverizer 24, The dilute sugar solution 37 produced by the cellulosic biomass saccharification unit 16 at the stage where the saccharification is performed in the first enzymatic saccharification tank 27 (including before the start of saccharification in the batch system) Supply. Thereby, the sugar concentration of the sugar liquid 22 obtained from the carbohydrate-based raw material 21 can be set to a predetermined sugar concentration (for example, 15% by mass). Moreover, since the use of the water for dilution can be suppressed by using the 1st sugar liquid 62 and the 2nd sugar liquid 64 as a dilution solution at the time of saccharifying the carbohydrate-type raw material 21, Costs required for manufacturing can be reduced.

Conventionally, when the carbohydrate-based raw material 21 is saccharified to produce the sugar liquid 22, half of the components contained in the carbohydrate-based raw material 21 is starch, and the sugar concentration of the sugar liquid when the carbohydrate-based raw material 21 is saccharified as it is is 20 % To 60%. When a sugar solution having a high concentration is used when alcohol is produced, it becomes an atmosphere with a high alcohol concentration as the fermentation progresses, and microorganisms are killed. Therefore, it cannot be used as it is for alcohol fermentation. Therefore, when the carbohydrate-based raw material 21 is saccharified to produce the sugar solution 22, it is necessary to dilute the carbohydrate-based raw material 21 with water to produce the sugar solution 22. On the other hand, when the biomass raw material 35 is saccharified to produce the sugar liquid 22, the biomass hydrothermal treatment product (solid residue fraction 39, hydrothermal extraction fraction 40) discharged from the biomass raw material 35 has a low concentration. The concentration of the heat-treated product (solid residue fraction 39, hydrothermal extraction fraction 40) is increased, or the first enzyme 61 and the first to the biomass hydrothermal-treated product (solid residue fraction 39, hydrothermal extraction fraction 40) It was necessary to increase the amount of the second enzyme 63 added, and to increase the sugar concentration of the first sugar liquid 62 and the second sugar liquid 64 obtained to prepare the sugar liquid 22.

On the other hand, according to the sugar liquid production apparatus 11A according to the present embodiment, the first sugar liquid 62 and the second sugar liquid 64 are used as a diluted solution when the carbohydrate-based raw material 21 is saccharified. Without increasing the sugar concentration of the sugar solution 62 and the second sugar solution 64, the sugar concentration of the sugar solution obtained from the carbohydrate-based raw material 21 is lowered, and the sugar solution 22 having a predetermined sugar concentration (for example, 15% by mass) is obtained. Can be produced. Moreover, use of the water used when saccharifying the carbohydrate-type raw material 21 can be suppressed. Thereby, it is possible to obtain a sugar solution 22 having a preferable concentration when performing alcoholic fermentation or the like, and to reduce the cost required for producing the sugar solution 22.

In the present embodiment, the first sugar liquid 62 and the second sugar liquid 64 obtained by saccharifying the solid residue fraction 39 and the hydrothermal extraction fraction 40 discharged from the hydrothermal decomposition apparatus 32A are used as the diluted sugar liquid 37. However, the present embodiment is not limited to this, but the first sugar solution 62 or the second enzyme saccharification tank 27 is supplied to one or both of the storage tank 25 and the first enzyme saccharification tank 27. The sugar solution 64 may be supplied as a diluted sugar solution 37 to one or both of the storage tank 25 and the first enzyme saccharification tank 27.

After the sugar liquid 22 is generated at a predetermined concentration in the first enzyme saccharification tank 27, the sugar liquid 22 as an alcohol fermentation raw material is supplied to the alcohol fermentation tank 12 through a sugar liquid supply line L12.

The alcohol fermenter 12 is a fermenter that adds the microorganism 65 to the sugar liquid 22 and ferments it to produce alcohol (organic raw material). The alcohol fermenter 12 is fermented under a predetermined condition by the yeast 65 added.

The alcoholic fermentation broth 71 subjected to the alcoholic fermentation is fed to the distillation column 13 through the fermentation broth supply line L13 and distilled. The distilled distillate 72 that has been distilled passes through the alcohol supply line L14 and is purified by a purifier such as a dehydrator 73, and is sent to the alcohol tank 14 and stored. An alcohol 74 such as ethanol as a product is supplied from the alcohol tank 14 through a supply line L15 as necessary.

The residue 75 in the alcohol fermenter 12 is discharged through the yeast residue discharge line L21. The distillation residue 76 in the distillation column 13 is discharged through a distillation residue discharge line L22, passes through a separator 77, a dryer 78, and a cooler 79, and is discharged as a distillation pad 800.

When the alcohol 74 is produced using the alcohol production system 10A, for example, when the production amount of the alcohol 74 is 100000 kl / year, the carbohydrate-based raw material 21 can be 90000 kl / year and the biomass raw material 35 can be 10000 kl / year. . Therefore, compared with the case where the alcohol 74 is manufactured using only the carbohydrate-based raw material 21, it is possible to manufacture the same amount of the alcohol 74 as the conventional one while suppressing the annual usage of the carbohydrate-based raw material 21.

As described above, according to the alcohol production system 10A including the sugar liquid production apparatus 11A according to the present embodiment, the diluted sugar liquid 37 derived from the biomass raw material 35 generated by the cellulose-based biomass saccharification unit 16 is used as the diluted sugar liquid supply pipe. L11 is supplied to one or both of the storage tank 25 and the first enzyme saccharification tank 27, and the diluted sugar liquid 37 is mixed at the adjustment stage before the sugar liquid 22 is generated from the carbohydrate-based raw material 21. Yes. Thereby, the production efficiency of the sugar liquid 22 obtained from the carbohydrate-based raw material 21 is improved, the sugar concentration of the sugar liquid 22 is set to a predetermined sugar concentration (for example, 15% by mass), and the cost required for producing the sugar liquid 22 Can be reduced. For this reason, when preparing the sugar liquid 22 derived from the carbohydrate-based raw material 21, the production efficiency of the alcohol 74 is improved by preparing the sugar liquid 22 having a predetermined sugar concentration using the diluted sugar liquid 37 derived from the biomass raw material 35. And the cost required for producing the alcohol 74 can be reduced.

In the present embodiment, examples of the carbohydrate-based raw material 21 include grains such as corn, rice, wheat, barley, and cassava, but the present invention is not particularly limited thereto.

For example, when corn 81 is used as the carbohydrate-based raw material 21, both the carbohydrate-based raw material 21 such as seeds and the cellulose-based biomass raw material 35 such as leaves, stems, and corn core are obtained from the corn 81. 22 can be manufactured more efficiently. FIG. 4 is a diagram illustrating an example in which corn 81 is used as a raw material. As shown in FIG. 4, both the carbohydrate-based raw material 21 such as the seed 81a and the cellulosic biomass raw material 35 such as the leaf, stem, and corn core 81b are obtained from the corn 81. For this reason, since the seeds 81a and the like can be used as the carbohydrate-based raw material 21, and the leaves, stems, and corn cores 81b can be used as the cellulose-based biomass raw material 35, according to the sugar liquid production apparatus 11A according to the present embodiment. The sugar solution 22 can be obtained more efficiently without producing waste from one raw material as in the case of corn 81, and the production of organic raw materials such as alcohol 74 can be made more efficient.

In the present embodiment, the case of performing alcoholic fermentation, which is an organic raw material, using the sugar liquid 22 as a fermentation system has been described. However, the fermentation system using the sugar liquid according to the present embodiment is not limited to this. However, the alcoholic substances (ethanol, methanol, etc.), which are organic raw materials, are exemplified as those obtained by fermentation treatment. However, the present invention is not limited to this, and is a raw material for chemical products other than alcohols. Amino acids to be used as petroleum substitutes or food / feed raw materials can also be obtained by a fermentation apparatus.

Examples of chemical products obtained from the sugar liquid 22 include LPG, fuel for automobiles, jet fuel for aircraft, kerosene, diesel oil, various heavy oils, fuel gas, naphtha, naphtha decomposition products such as ethylene glycol, ethanol, amine, lactic acid, Examples include alcohol ethoxylate, vinyl chloride polymer, alkylaluminum, PVA, vinyl acetate emulsion, polystyrene, polyethylene, polypropylene, polycarbonate, MMA resin, nylon, and polyester. Therefore, it is possible to efficiently use the biomass-derived diluted sugar liquid 37 as a substitute for a chemical product derived from crude oil, which is a depleted fuel, and as a raw material for producing the substitute.

A sugar solution production apparatus according to Example 2 of the present invention will be described with reference to the drawings. FIG. 5 is a schematic view of an alcohol production system including a sugar liquid production apparatus according to Example 2 of the present invention. In addition, since the sugar liquid manufacturing apparatus which concerns on a present Example is the same as that of the structure of the alcohol manufacturing system provided with the sugar liquid manufacturing apparatus which concerns on Example 1 of this invention shown in FIG. 1, it is the same member as Example 1. For the above, the same reference numerals are given, and redundant description is omitted.

As shown in FIG. 5, the alcohol production system 10 B includes a sugar liquid production apparatus 11 B, an alcohol fermenter 12, a distillation tower 13, and an alcohol tank 14 according to the present embodiment.

The molasses production apparatus 11B according to the present example uses molasses 83 as a saccharification raw material obtained from the carbohydrate-based raw material 21 of the molasses production apparatus 11A according to Example 1 of the present invention shown in FIG. That is, the sugar liquid production apparatus 11B according to the present embodiment includes a sugar liquid adjusting unit 15B and a cellulose biomass saccharification unit 16.

The sugar liquid adjusting unit 15B is for manufacturing the sugar liquid 22 from the molasses 83. The sugar liquid adjustment unit 15 B includes a storage tank 25 and a sugar concentration adjustment tank 84. Molasses 83 is extracted or extracted from the carbohydrate-based raw material 21. Molasses 83 obtained from the carbohydrate-based raw material 21 is stored in the storage tank 25. The sugar concentration of the molasses 83 stored in the storage tank 25 is adjusted in the sugar concentration adjusting tank 84.

The cellulose-based biomass saccharification unit 16 is the same as the sugar liquid production apparatus 11 according to Example 1 of the present invention described above, and thus the description thereof is omitted.

The diluted sugar solution 37 produced in the cellulose biomass saccharification unit 16 is supplied to either or both of the storage tank 25 and the sugar concentration adjusting tank 84 through the diluted sugar solution supply pipe L11. Thereby, the diluted sugar liquid 37 can be mixed with the molasses 83 obtained from the carbohydrate-based raw material 21. That is, in the sugar liquid adjusting unit 15B, the diluted sugar liquid 37 generated in the cellulosic biomass saccharification unit 16 is supplied to the molasses 83 in the adjustment stage before the sugar liquid 22 is generated from the molasses 83 obtained from the carbohydrate raw material 21. To do.

Thereby, the sugar concentration of the molasses 83 obtained from the carbohydrate-based raw material 21 can be set to a predetermined sugar concentration (for example, 15% by mass). In addition, since the first sugar liquid 62 and the second sugar liquid 64 can be used as a diluting solution when saccharifying the carbohydrate-based raw material 21 and the use of water for dilution can be suppressed, Costs required can be reduced.

Therefore, according to the sugar liquid production apparatus 11B according to the present embodiment, the first sugar liquid 62 and the second sugar liquid 64 are used as a diluted solution when the sugar liquid 22 is produced from the molasses 83, so that the first Without increasing the sugar concentration of the sugar solution 62 and the second sugar solution 64, the sugar concentration of the molasses 83 obtained from the carbohydrate-based raw material 21 is lowered, and the sugar solution 22 having a predetermined sugar concentration (for example, 15% by mass) is obtained. Can be produced. Moreover, use of the water used when producing the sugar liquid 22 from the molasses 83 can be suppressed. Thereby, it is possible to obtain a sugar solution 22 having a preferable concentration when performing alcoholic fermentation or the like, and to reduce the cost required for producing the sugar solution 22.

Therefore, according to the alcohol production system 10B including the sugar liquid production apparatus 11B according to the present embodiment, when the molasses 83 derived from the carbohydrate-based raw material 21 is adjusted, a predetermined sugar is used using the diluted sugar liquid 37 derived from the biomass raw material 35. By producing the sugar solution 22 having a concentration, the production efficiency of the alcohol 74 can be improved and the cost required for producing the alcohol 74 can be reduced.

In this embodiment, the case where molasses is used as the saccharification raw material obtained from the carbohydrate-based raw material 21 has been described. However, the present invention is not limited to this, and for example, the carbohydrate-based raw material 21 such as sugar cane and sugar beet is used. What is necessary is just to be obtained by extracting or exploiting.

For example, when sugarcane is used as the raw material, molasses is obtained from the sugarcane as the carbohydrate-based raw material 21, and the cellulose-based biomass raw material 35 such as a residue (bagasse) obtained by extracting sugar from the leaves or sugarcane is obtained. Furthermore, it is possible to manufacture efficiently. FIG. 6 is a diagram illustrating an example in which sugarcane is applied as a raw material. As shown in FIG. 6, from sugarcane 85, both molasses 83 and cellulosic biomass material 35 such as leaves and bagasse 85a are obtained as carbohydrate-based material 21. For this reason, molasses 83 can be used as the carbohydrate-based raw material 21 and leaves, bagasse 85a and the like can be used as the cellulose-based biomass raw material 35. Therefore, according to the sugar liquid production apparatus 11B according to the present embodiment, from one raw material, The sugar liquid 22 can be obtained more efficiently without producing waste, and the production of organic raw materials such as alcohol 74 can be made more efficient.

10A, 10B Alcohol production system 11A, 11B Sugar solution production equipment 12 Alcohol fermentation tank 13 Distillation tower 14 Alcohol tank 15A, 15B Sugar solution adjustment part 16 Cellulose biomass saccharification part 21 Carbohydrate raw material 22

Sugar solution

23, 31 Crusher 24 Fine Pulverizer 25 Storage tank 26 Steamer 27 First

enzyme saccharification tank

32A, 32B Hydrothermal decomposition apparatus 33 Second enzyme saccharification tank (C6)
34 Second enzymatic saccharification tank (C5)
35 Cellulosic biomass material (biomass material)
37 Diluted sugar liquid 38 Biomass raw material pulverized product 39 Solid residue fraction 40

Hydrothermal extraction fraction

41, 51

Biomass supply device

42, 52 Reactor 43 Biomass extraction device 44 Screw means 45 Pressurized hot water 47 Dehydrated liquid 48 Pressurized Nitrogen (N ₂ )
49 Temperature jacket 53 Fixed stirring means 61 First enzyme (cellulase)
62 First sugar solution 63 Second enzyme 64 Second sugar solution 65 Microorganism 71 Alcohol fermentation solution 72 Distillate 73 Dehydrator 74 Alcohol 75 Residue 76 Distillation residue 77 Separator 78 Dryer 79 Cooler 80 Distiller 81 Distiller 81 Corn 83 Molasses 84 Sugar concentration adjustment tank 85 Sugar cane L11, L11-1 to L11-5 Dilute sugar solution supply pipe V11, V12, V21, V22 Control valve V31 to V35 Differential pressure adjustment valve (ON-OFF valve)

Claims

A sugar solution production apparatus for producing a sugar solution derived from a carbohydrate-based raw material,
A sugar solution adjusting unit for adjusting the sugar solution derived from the carbohydrate-based raw material;
A cellulosic biomass saccharification part for producing a dilute sugar solution by saccharifying a biomass hydrothermal treatment product obtained by hydrothermal decomposition of a cellulosic biomass raw material containing a lignin component and a hemicellulose component;
A diluted sugar solution supply pipe for mixing the diluted sugar solution produced in the cellulose biomass saccharification unit with the sugar solution adjusting unit;
An apparatus for producing a sugar solution, comprising:
In claim 1,
The sugar solution production apparatus according to claim 1, wherein the sugar solution is obtained by saccharification of the carbohydrate-based material, or extracted or extracted from the carbohydrate-based material.
In claim 1 or 2,
The cellulosic biomass saccharification part is a hydrothermal decomposition apparatus that hydrothermally heats the cellulosic biomass raw material to produce a biomass hydrothermal treatment,
A second enzyme saccharification tank for adding an enzyme to the biomass hydrothermal treatment to saccharify the biomass hydrothermal treatment to produce the diluted sugar solution;
An apparatus for producing sugar solution.
In claim 3,
The hydrothermal decomposition apparatus hydrothermally decomposes the cellulosic biomass material in contact with pressurized hot water, transfers a lignin component and a hemicellulose component into the pressurized hot water, and from the cellulosic biomass material Separating the lignin component and the hemicellulose component;
An apparatus for producing a sugar solution that generates a hydrothermal extraction fraction containing the lignin component and a hemicellulose component and a solid residue fraction containing a cellulose component as the biomass hydrothermal treatment product.
In claim 4,
The second enzymatic saccharification tank adds an enzyme to the solid residue fraction discharged from the hydrothermal decomposition apparatus, enzymatically decomposes the cellulose component in the solid residue fraction, and contains a 6-carbon sugar. And a dilute sugar solution containing pentose by adding an enzyme to the hydrothermal extraction fraction discharged from the hydrothermal decomposition apparatus, and enzymatically decomposing the hemicellulose component in the hydrothermal extraction fraction An apparatus for producing a sugar solution that produces either or both.
In any one of claims 1 to 5,
An apparatus for producing a sugar solution, wherein the sugar concentration of the diluted sugar solution is 0.1% by mass or more and 15% by mass or less.
A sugar solution production apparatus according to any one of claims 1 to 6,
An alcoholic fermenter that ferments the sugar solution to produce organic raw materials;
A fermentation system comprising:
A sugar solution production method for producing a sugar solution derived from a carbohydrate-based raw material,
A biomass biomass raw material containing a lignin component and a hemicellulose component is hydrothermally decomposed to produce a biomass hydrothermal treatment product, and an enzyme is added to the obtained biomass hydrothermal treatment product to saccharify the biomass hydrothermal treatment product, thereby dilute sugar Manufacturing the liquid,
A method for producing a sugar solution, wherein the sugar solution is produced by using the diluted sugar solution when preparing the sugar solution derived from the carbohydrate-based raw material.
In claim 8,
A method for producing a sugar solution, wherein the sugar solution is obtained by saccharification of the carbohydrate-based raw material or by extraction or extraction from the carbohydrate-based raw material.
In claim 8 or 9,
The cellulosic biomass raw material is hydrothermally decomposed in contact with pressurized hot water, the lignin component and hemicellulose component are transferred into the pressurized hot water, and the lignin component and hemicellulose component are separated from the cellulosic biomass raw material. Producing a hydrothermal extraction fraction containing a lignin component and a hemicellulose component, and a solid residue fraction containing a biomass solids,
A method for producing a sugar liquid, wherein one or both of the hydrothermal extraction fraction and the solid residue fraction are used as the biomass hydrothermal treatment product.
In claim 10,
As the dilute sugar solution, an enzyme is added to the solid residue fraction, the cellulose in the solid residue fraction is enzymatically decomposed, and a dilute sugar solution containing hexose is added to the hydrothermal extraction fraction. , A method for producing a sugar solution using any one or both of a dilute sugar solution containing pentose by enzymatic degradation of a hemicellulose component in the hydrothermal extraction fraction.
In any one of claims 8 to 11,
A method for producing a sugar solution, wherein a sugar concentration of the diluted sugar solution is 0.1% by mass or more and 15% by mass or less.
A fermentation method comprising fermenting a sugar solution obtained by using the sugar solution production method according to any one of claims 8 to 12 to produce an organic raw material.